Method and apparatus for distillation of oil



Feb. 4, 1936- A. G. PAGE 2,029,51

METHOD AND APPARATUS FOR DISTILLATION OF OIL Filed Sept. 26,v 1923 INVENTOR. flZexazzcZer @fia ge Q ATTORNEY.

Patented Feb. 4, 1936 UNITE ATES eArN OFFICE METHOD AND APPARATUS FOR DISTIL- LATION 0F OIL Application September 26, 1928, Serial No. 308,500

31 Claims.

Distillation process involving vaporization of a complex liquid, followed by a rectification of vapor including heat recovery steps from the various parts of operation necessitates accurate control of the various factors entering into the distillation and rectification stages.

The following controls are essential to obtain proper conditions for distillation and rectification:

The temperature of the oil undergoing vaporization must be controlled. In the vaporization of a complex mixture, such as crude oil or petroleum fractions, the composition of the vapors rising from the liquid depends upon the temperature of the liquid undergoing vaporization.

In order to produce a maximum yield of a given product, it is essential that the temperature be high enough not only to vaporize this product from the liquid, but to vaporize also a considerable proportion of the heavier bodies. This is due to the fact that at any given temperature vapors rising from the complex liquid have a composition depending upon the partial pressure of the various components in the liquid and therefore upon the relative proportion of these components in the liquid. Having formed the vapors at a temperature sufiiciently high to insure the vaporization of the components desired, it is necessary to separate the vapors into the desired and undesired components. This is accomplished by rectification. As is well known to those skilled in the art, in order to obtain a product having the desired quality, the vapors issuing from the rectification system must be at a definite and predetermined temperature. To produce this temperature, the partial condensation upon which is depended to obtain the reflux necessary to the rectification stage must be controlled so that the temperature of the vapors exiting from the partial condenser shall be at the desired point. Stating it in another way, in order to obtain a resultant liquid as an overhead from an overhead vapor from the rectification column, the composition of the vapor entering the column and the composition of the reflux returned to the top of the column must be controlled in quality. The former is controlled by controlling the vaporization of liquid and the latter is controlled by controlling the condensation of the vapors issuing from the column, that by controlling the temperature of the condensation.

If a system is to be in constant equilibrium, all the various factors must be invariant, or must vary in a definite relationship. Should any one of these controls vary, even slightly, the system is unbalanced and the fractions obtained are not the ones desired. In order to re-establish equilibrium, the variation must be corrected or the other factors must be varied in a definite manner.

It is the object of this invention to devise a process and apparatus by which distillation will be controlled entirely automatically and conditions once fixed will be constantly maintained irrespective of any variation which may occur accidentally, or the variation will be met by an automatic variation of the rest of the factors to re-establish equilibrium.

The essentials of good heat utilization in a distillation process involves the recovery of heat from the products and imparting this heat to the incoming charging stock. The use of charging stock as a cooling medium for the vapors in the condensation stages has been suggested. Two difliculties arise from such use, especially if the material is partially volatile at the temperature of condensation as is the case in distillation of crude oil or volatile liquids. One is that the stock at the temperature of condensation usually vaporizes partially. Another is that the cooling is dependent upon the rate of the feed. I have found that automatic control of condensation and, therefore, of rectification, is materially facilitated and made practical if the cooling medium can be controlled independently of the rate of feed and, also, the automaticity of the process is also materially facilitated and made practical if the cooling medium is substantially non-volatile at the temperature of condensation.

- It is, therefore, an object of this invention to eliminate all variables from the distillation process so that conditions, when once fixed, shall remain constant.

Broadly stated, my invention comprises regulating the heating of the oil so as to maintain the oil automatically at a given temperature and be vaporized thereby; regulating the partial condensation of vapors from the rectifier so as to maintain a reflux to the rectifier at a constant and appropriate temperature for the composition of the product desired, or by automatically varying the several factors so as to obtain constant equilibrium conditions by circulating the cooling fluid at a controllable rate, independent of the in-put rate of the feed and, also, using a cooling fluid of a non-volatile character at the temperature of condensation.

One of the specifically preferred embodiments which is inducive of the success of my invention is the cyclic circulation of the substantially nonvolatile cooling medium through the condenser, through a cooling medium, into a storage and back to the condenser. By providing this cyclic circulation of a substantially non-volatile fluid, the above condensing conditions are obtainable.

Stating it more specifically, the invention resides in a distilling and condensing system, pref erably for petroleum oil or like complex liquid, wherein a cooling liquid is used for condensation purposes and is cyclicly circulated through a closed circuit, said liquid being non-volatile at the temperatures employed so as to completely avoid volatilization thereof in every part of the system, the circulation of the liquid being controlled to regulate the rate of heat exchange and to insure proper temperature ranges in the various stages with consequent production of the desired fractions.

In a preferred embodiment, the temperature control is automatic. The rate of heat exchange may be regulated by controlling the rate of circulation of the cooling liquid through the cooling circuit, as by means of automatic temperature controlled flow regulators which insure exactly the desired amount of cooling in each cooling or condensing device employed in the system. Preferably heat is applied to preheat the feed stock in proportion to the amount of heat absorbed in the condensation stages, and in a practical embodiment this is accomplished by cooling the cooling liquid by heat exchange with the feed stock. Two functions are thereby accomplished, namely, preheating the feed and properly cooling the circulating cooling liquid.

This invention will be better understood by reference to the accompanying drawing which shows a schematic arrangement of an apparatus for carrying out this process;

Charging stock, such as crude oil, contained in tank I passes by pump 2 through line 3 and split through line 4 and loaded valve 5 and through thermostatically controlled valve 6 to pass in parallel through heat exchangers 9 and I2 and through lines II and M to unite in line I5. In line H is positioned a pyrometric element l0 and in line I4 is positioned a pyrometric element l3. I0 is connected by l to the upper side of the diaphragm of the differential thermostatic valve 6 while I3 is connected by line 8 tothe under side of diaphragm valve 6. This valve is further described herein.

The oil in line I5 is passed through heat exchanger !6 to be introduced in vaporizer l8. Unvaporized material passes from l8 through valve 20 controlled by level control 19 which acts to maintain a predetermined level in l8. The centrifugal pump 2| is of sufiicient capacity to take the maximum amount of oil to be removed from I8 and therefore cooperates with level control l9 to maintain the oil at the proper level in i8. Pump 2| then passes the oil through heat exchanger element 22 and line 23. The vapors from l8 pass to line 24 to be introduced into fractionating column 25. The condensate in this fractionating tower passes through 21 controlled by the level control 26 and through pump 28 to be united with the oil in 29 from 2| to pass through 22. The overhead vapors from the fractionating tower 25 pass through line 30 into partial fractionating condenser 3| to form a condensate which is returned by centrifugal pump 32. The uncondensed material then passes through 33 to be condensed in condenser 34. The commingled stream in line 23 passes into exhausting column 35. The tower acts both as an exhauster and a rectifying column. In the upper part of the column, i. e. above the point of introduction of 23 it is a rectifying column. The liquid material in 35 collects in the bottom thereof and is controlled by level control 36 and valve 31 and is passed by the centrifugal pump 38 through heater coil 40 positioned in furnace 4| which is heated by burner 43, fuel to which is controlled by the thermostatically controlled valve 44 responsive to the pyrometric element 42 on the discharge side of the coil. The heated oil then passes through 45 into vaporizer 46. The unvaporized residuum collects in 46 regulated by a level control 41 and is discharged through valve 48 by pump 49 into line 50 passing to heat exchangers 5| and 52 and 54 via 53 to be discharged to storage or to further treatment. The vapor issuing from 46 passes through line 55 to be introduced into the bottom of exhausting column 35, passes countercurrent to the oil introduced via 23. The overhead vapors pass in line 56 into the fractionating column 51. The reflux condensate in 51 maintained to a proper level by level control 58 discharges through valve 59 by way of centrifugal pump into the top of the exhausting column 35 to act as a reflux and be revaporized. Vaporized material from 51 passes to partial condenser 62 and condensate is returned by way of centrifugal pump 63 as a reflux to 5! via line 64. The uncondensed material from 52 passes to 65 and is condensed in condensers 5o, 51. 61 may be either a condenser or a cooler.

Provision is made for drawing off a fraction of the liquid returned from 51 if this is desired. By-pass valves 8'! and 88 are provided to operate the by-pass 89. Valve 81 is closed and 88 is opened. In by-pass 89 is a thermostatic valve 90 responsive to the pyrometric element 9| in line 56. A by-pass and loaded valve 92 is also provided.

The cooling circuit will now be described.

The cooling medium is maintained in tank 68 and is pumped by pump 69, the operation of which is controlled by throttle valve 10 on the steam line to the pump. This valve 18 is responsive to a pyrometric element H positioned on the discharge side of the pump 69. Cooling medium is then pumped through 12 and is split through loaded valve 13 and thermostatically controlled valve 74 responsive to pyrometric element 15 positioned in line 33. Part of the stream, therefore, passes through 16 in indirect heat exchange and out of contact with the vapors passed into partial condenser 3| and unites with the stream passing through 13 in 11. The combined stream then passes through coil 18 also out of contact with the vapors passed into condenser 66 and then into line 19 and is split by way of loaded valve 83 and thermostatically controlled valve 80 responsive to the pyrometric element 8.: positioned in line 65. The stream, therefore, passes through 82 in indirect heat exchange and out of contact with the vapors passed into partial condenser 52 and unites with the stream through 83 in line 84. The combined stream then passes through cooling coil 85 in indirect heat exchange and out of contact with crude oil passed into heat exchanger 9 and is returned via 86 to the tank 68.

Mention may be made of the character of the thermostatic control valves 44, 10, T4, 80 and 9B. These are any of the well known thermostatic valves which operate to open and close responsive to a change of temperature. They may be of the pressure diaphragm type wherein a rise temperature, or :vice versa. Such valves are a common type as will be recognized by those skilled in the art. .As: shown, all of the valves operate to open on increasein temperature at their respective ipyrometric elements. When the temperature drops they will close fa predetermined amount. The-amount of opening at :any temperature and the degree :of opening for any rise in temperature can be set on these valves. Such valves are well known. In the -drawing, the valves are shown schematically only.

The valve B is of a balanced valve of the above type wherein the pressure from two pyrometric elements -is directed opposite --each other against the diaphragm. The valve will then open and close responsive to difference in :pressure and, therefore, difference in temperature at these points, specifically as shown at H) and 13. The amount and direction 01' opening --or closing of the valve will depend upon the difference in temperature. As shown, if in is at a higher temperature than 1.3, the valve will close, if I3 is higher than H), the valve will open. Such valves are well known.

The loaded valves 5, I3, -83 and 92 are ordinary loaded valve or block valve type, which create a back pressure to aid operation of the thermostatic valves. The level control 1.9, 26, 36, ll, and 58 operating valves 20, 21, 31, 48 and 59 are of conventional types.

The operation of the device is as follows: (A specific example will be given to aid in the explanation, but it will be understood that this example is merely an illustration to indicate the operaton of the device and process and not a limitation of my invention) Crude oil of 28 A. P. I. at apredetermined rate is passed through line 3 and is split through exchangers 9 and I2. Valves 5 and 6 are so set that the temperatures at l3 and Ill shall be maintained the same. In 9 the oil is heated by the heated cooling medium passing through .85 and in i 2 it is heated by the partially cooled residuum passing through 54., In other words, the stream is split so that the heat picked up by each fraction will raise the temperature of each stream to the same level, for example, the temperature at H) and I3 will be substantially 160 F. The combined stream will then pass through heat exchanger |6 to pick up as much heat as possible from the residuum passing through 52. The temperature of the oil passing through I'G will be raised to approximately 345 'F.

The thus preheated oil is then introduced into the primary ,vaporizing column i3 Where it is flashed to remove the material volatile at that temperature. The vaporized material is then fractionated in rectifying column 25. This rectification is controlled by the control of the cooling fluid so that the vapor temperature is 175 F. All of the reflux formed in the partial condenser is returned by means of centrifugal pump 32, which is of sufficient capacity to take the maximum flow. The unvaporized material from the vaporizer l8 and the liquid condensate in are passed respectively through pumps 21 and 28, and passed through exchanger 22 and introduced into the exhausting column 35. The provision of the level controls l9 and 26 and the provision of the centrifugal pumps 21 and 28 ensures the constant passage of all liquid irrespective of the variations in :flow. The liquid from vaporizing tower 3511s then passed through pump so into the heatingcoil 40. The heating of this coil $3 is so controlled by thep'yrometric element 52 and valve it to produce .an exit temperature at 42 at 580. The unvaporized residuum withdrawn by 49 is passed :to heat exchangers .54, I6 and l2. The vapors from it enter into to pass countercurrent to the liquid therein and the vapors from 35 are fractionated in'Ei'l' as previously described, the fractionationibeing so controlled by means of cooling fluid passing through '82 to maintain vapor temperature at 8i of 340 F. It will be seen as describedthis process produces three fractions; a primary light :gasoiineat 34 of about 60 A. P. 1.; a heavier gasoline at 6-7 of 46 A. P. I.; anda residuum through *53 of about 18 A. P. I. It will be obvious to theiman skilled in the art that addi tioral fractions :could be withdrawn, as for instance, instead of returning the fractions through 60 130135, this may be sent to storage to produce a gas oil fraction 01- fractions of that character. Topermit'this, valve-311s closed and 88 is opened and reflux is returned to column 35 in order to maintain a predetermined temperature at 9 i, and the rest sent by the by-pass valve 92. In the specific example given no gas oil is removed, the system being operated to produce two grades of gasoline and fuel oil. If a gas oil out is desired, the temperature on'the outlet of the oil heater is raised to 625 F. and the reflux to tower '35 is so controlled .as to maintain a temperature at 8! equal to 475 F. Additionally, by raising the temperature-at t2 and a provision of several fractionating columns, such as 5! in series, various lubricating cuts, gas oil cuts and fractions may be obtained if a proper crude is being distilled. Care must be taken in this latter case so that the temperature of the residuum passes through the various heat interchanges which shall not be too low to congeal the same. This will be obvious 'to those skilled .in the tart.

Attention "is-now drawn to the operating features 'of this invention by which this process is maintained automatic.

One of the important factors which makes the constant equilibriumpossibleis that the condensing characteristics in this system automatically compensate for any fluctuations in character or material to be condensed and in such sporadic variables as atmospheric temperatures. It is obvious that in the design of a system the condensingcapacity and function must be fixed. This is usuallydeterminedby providing an adequate condensing surface at the requisite place. In determining the amount of condensing surface the heat absorptive characteristic of the cooling fluid passing throughcooling tubes must be known. This must remain invariant, otherwise, the original design will not meet the conditions. Thus, if a cooling fluid vaporizes in the tubes, we would no longer have the predetermined heat interchange since the absorptive characteristic of a mixture of vapor and liquid passing through a tube is entirely difierent'from that of a liquid alone. When this vaporization occurs, the heat absorption is.

sporadic and non-controliable. The requirement as above described is, therefore, to maintain the heat absorption characteristic of the condensing material constant by providing heat absorption fluid which Will not vaporize to any appreciable amount at the temperature of condensation. When so provided, condensation is absolutely controllable to produce condensing temperatures at any desired fixed point, it being merely necessary to increase the rate of flow in a predetermined manner. The heat absorption characteristic being flxed, a definite increase in volume or flow will cause a predetermined increase of ab sorption of heat. Provision is made, therefore, in this system for automatically varying the rate of flow through the condensing surface to maintain any exit temperature at a predetermined level by using a cooling fluid which will not vaporize at the temperature of condensation. However, since the amount of cooling fluid necessarily depends not only upon the heat it must absorb, but also upon its entering temperature into the heat exchange surface, provision is made for varying the rate of flow responsive to its own temperature. This is provided in this system by controlling the operation of circulating pump 69 by means of a pyrometric element ll. As the temperature at H rises valve 10 opens to speed up the pump a predetermined amount in accord with the said rise of temperature. The original design of this system is such that the amount of material to be circulated from 68 is regulated to provide the requirement for the total heat absorbing surface. The variation in amount of cooling fluid necessary in relation to the varying temperatures of the cooling fluid 58 is easily determined as will be obvious to those skilled in the art. The valve ill and the thermostatic element "II are so set that the correct amount of cooling fluid is circulated for any temperature thereof.

Since the quality of the fractions produced depends upon the vaporizing temperature of the liquid undergoing distillation and on the temperature of the vapor exiting from the partial reflux condenser of the fractionating column, controls at these two points are essential for constant equilibrium. In the system as described, the distillation temperature is regulated by controlling the exit temperature from the heater. No effort is made to control the primary vaporization in I8. The latter merely acts to remove any vapors formed. Provision, however, is made to segregate from the vapors thus formed only those that may be desired. The rest is returned to the second distillation stage in which vaporization is controlled as described above. This simplifies the system and takes advantage of efficient heat recovery.

The next stage of control to make the system produce the fractions of desired quality is the control of fractionation. This is made possible by controlling the vapor temperature leaving the partial reflux condenser by passing the requisite amount of cooling fluid therethrough.

Provision is therefore made for this by providing a thermostatically controlled valve in the line and a by-pass. The loaded valve on the by-pass permits of accurate working of this thermostatic valve and to pass an amount of cooling fluid suited to the requirements therefor.

The provision of centrifugal pumps on the reflux return lines makes possible the return of all the reflux irrespective of the amount formed without any attention. They are of such capacity and run at such speed as to return the maximum amount formed. Then any fluctuation is taken care of.

The circulation of a proper amount of cooling fluid automatically responsive to the temperature desired to be obtained will obtain the desired control.

The heated circulating fluid is then returned to the cooler 85 in a closed cycle into tank 68. It is obvious that the temperature in 68 will,

therefore, depend not only upon fluctuation in heat absorption occurring in the various condensers but also upon the rate of flow of the oil through the cooler 85. It is to provide for these fluctuations that the control of the pump 69 is herein shown. In the specific example the maximum temperature which is attained by the circulatory fluid is at 82. (In the specific example the temperature of the vapors at this point is about 380 F.). A gas oil fraction having an initial boiling point above this temperature may be used as the circulating cooling fluid. Should much higher temperatures be desired and cooling fluids which do not vaporize at such temperatures be unavailable, the fluid may be kept under suflicient pressure to maintain it in liquid phase.

Attention is also called to the provision for the maintenance of equal temperatures at points I0 and I3. By maintaining the temperature at I0 and [3 identical, the cooling effect at 54 and 85 will be maintained at its maximum level. The functions of the feed as a cooling fluid in these heat exchangers is two-fold; one, to cool the circulating cooling fluid from 84 to as low a point as possible; two, to pick up as much heat from 54 as possible. Since the operation of one is at the expense of the other, the optimum balance is maintained by providing an equal temperature at 10 and I3. The combined stream is then passed through 16 where it is allowed to pick up whatever heat it can. The further heating or" oil is thereafter controlled to maintain constant exit temperature at 42 as described. There is a maximum conservation of heat since the cooling fluid circulates in cyclic fashion and all the heat imparted to the oil in the heater 4| and 52 except that lost by radiation, an amount which is reduced to a minimum by insulating the system, is returned to the incoming crude by an independent circulating system. The independent circulatory system has the additional feature that the heat in the vapors is imparted to the incoming feed without causing the condensation to be dependent on the flow of incoming feed. If the DICOIIliI." feed were to be used as the vapor cooling fluid, fluctuations'in flow of feed would cause fluctuations in condensation which would act to make automatic control diiiicult, if not impossible.

It will be seen that as herein described, the distillation system is absolutely automatic and fractions of constant characteristics are obtained, and since it is automatic, the operation will be at maximum efiioiency. Any fluctuations which may occur in the flow of the oil, or accidents in condensation, such as always occur by variations in atmospheric temperature, are automatically compensated.

It remains but to describe the operation of the system when the quality of the crude oil or the material to be distilled changes. It will be understood that in the distillation of a complex mixture such as crude oil or any liquid composed of a large number of fractions the composition of the vapors formed depends both on the temperature and the relative proportions of the various fractions in the material to be distilled. In the above system, the temperature of distillation is always sufficiently high to insure the vaporization of not only the desired gasoline and gas oil fractions but considerable of the fractions heavier than gas oil. Suppose then the crude oil changes so as to contain a smaller percentage of gasoline. fractions; If. the. controls. on the system are not altered, itlwill appear immediately that a. larger proportion of the oil will be re,- moved from thesystem asresiduum and a smaller proportion of theoil wilt be condensed. as-gasoline in condensers? and 62. Itwill' then be obvious that the crude oil passing, into. vaporizer is. will be at a higher: temperature. than. previously, due to the fact. that it is now in heat exchangewith a larger amount. of residuum. Consequent- 1y, with controlled refluxing to produce the desired gasoline in. 34., it would necessarily follow" that the temperature of the oil' introducedinto; vaporizer 35 increases andcagreater proportion of the material is being.- recycled through. the heater. The tendency, therefore, is toincrease the. vaporization inv 35 andto ensure sufficient. vaporization of the desired fractions. The same occurs when the crude. becomes richer in: gasoline. In this case the residuum is smaller in proportion while the. vapors are; in larger quantity in proportion- The crude oilis; then heatedup to a smaller degree than. previously while the.- circulating fluid is forced to. abstract. more. heat. than previously and this isrprovidedby the-automatic control on pump: 69:. The. temperature of the material. entering; 35 through 23 is then diminished, but due to the fact that it contains a larger percentage of light bodies. a proper amount of vaporizationoccurs butany accumulation of. light. bodies is prevented by circulating through heater 40, which: as described before is. at atemperature. to insure vaporization of. light bodies.

If the system is run by removing fractions through 92-. then if the; oil decreases in gasoline content without increase of temperature in the heatera greater proportion of .thisgas-oil portion may-be found in the residuum. In like manner, if the gasoline content of the crude chargedin creases, then sincefagreater proportion of the gasoil is vaporized: and enters the tower 5'1, stripping of the chargingstock is moreefiicient.andagreater proportion of: the stock is removed through 92; It is obvious, of course, that this automatic co-ntro l assumes that the crude does not vary to a very great extent in composition. Should, however, this. occur, such as for instance, if a very heavy oil isto berun instead of acrude .oil con-- taining an average amount of gasoline, then the original setting of the temperature at 42 may not be sufficient to produce the necessary vaporization but the system need be varied merely by increasing the temperature at 42- without any other alteration to be operative for this material. It will be advisable, probably, when the charging, stock changes in any material degree that this change of temperature at 42 be made in order that the system will run most efliciently. Since it is usual to charge this system from a tank and to switch to a second tank when that is empty and the characteristic of the material in each.

tank is known there need be no difficulty. However, the system will be maintained in equilibrium at all times and it will only be necessary to reset the temperature, andthe process will continue from there on: at the new-conditions'withoutinterruption. In previous systems a change-over from one set of. conditions to another meant the'destruction'ofthe original-equilibrium and a period;

of waiting until the new equilibrium was. established. During this period, which was always material',. the: system is out of equilibrium and the products are not usable.

The above is not to be taken as limiting my invention, but merely illustrative thereof. Va-

rious modifications and adaptations will occur to those skilled in the art within the scope of my invention. I claim:

1. A method: of distillation which comprises.

vaporizing a liquid, condensing the vapors by heat exchange with a coolingfluid and preheating the liquid, passing tov said vaporization, by heat exchange with the cooling. fluid passing from said heat exchange with said vapors. Y

2.. Av method: of distillation which comprises vaporizing a liquid, condensing the vapors by heat exchange with a cooling fluid, circulating said cooling fluid. through said heat exchange from a bulk supp-iy' to. said heat exchange, pre-heating the liquid passing to said vaporization by heat exchange with the cooling fluid passing from said first mentioned heat exchange, and returning said coolingi'luid to said bulk. supply.

3. A method of distillation which comprises vaporizing a liquid, condensing the vapors by heat exchange a cooling fluid and preheat.- ing. the liquid passing. to. said vaporization by indirect. heat exchange and out of contact with the cooling. fluid passing" from said heat exchange with. said vapors.

4.. A method of distillation which comprises. vaporizing an oil", condensing. the oil vapors by heat exchange. with a. cooling oil and preheating the oilipassing; to said: vaporization by indirect. heat exchange: and outioficontact with thecooling' oil' passing from. said heat. exchange with. said oil vapors;v

5'. A. method of distillation which comprises. vaporizing. a liquid,.condensing the vapors by in.- direct heat. exchange and out of contact with. a cooling fluid and preheating the liquid: passing. to; said. vaporization by indirect heat exchange and; out; of contact:with thercooiing fluidpassing from said indirect heat exchangev with. said vapors.

6.. A method. of distillation which comprises; vaporizing an oil, condensing the oil. vapors: by indirect. heat exchange and out of contact. with a cooling oil. and preheating the. oil passing: to said vaporization by indirect heat exchange and out. of; contact: with; the. cooling oil; passing. from: said indirect. heatzexchange with; said oil. vapors.

7.. A. method of. distillation. which" comprises; vaporizing. a.liquid,. condensing. the. vapors. by in.- direct. heatsexchan'ge: and. out of. contact with a. cooling fluid, circulating said. cooling fluid: through: said heat exchange.v from. a. bulk supply to. said heat: exchange, preheating the liquid passing; to said. vaporization: by indirect: heat; ex.-

change; and' out; of contact: with. the cooling fluid.

passing from said first: mentioned heat exchange, andretiurning said coolingv fluidlto. said bulk supply.

8. A. methodaof' distillation which comprises vaporizing. aliquid .to. form a vapor, rectifying said; vapor; partially condensing the:vapor to form a refluxior said rectification step,. by heat ex: change with a circulating. cooling. fluid, preheating the. liquid. passing to said vaporization. stage by heat. exchange with. said cooling; fluid passing from; said. partiall condensation stageand controlling the; said partial condensation by regu.- lating the rate of circulation of thecooling. fluid; independently of the rateofi said feed.

9'. A method: of distillation which comprises vaporizing. a liqiiidt to. form a vapor, rectifying said vapor, partially" condensing thevapor' to form a; reflux-J for: said: rectification-step, by heat exchange with a circulating cooling fluid, and automatically regulating the flow of cooling fluid in heat exchange With said vapors by automatically icy-passing a regulated portion of said cooling fluid to maintain the temperature of the unoondensed vapors at a constant and pre-determined point, pre-heating the liquid, passing to said vaporization stage, by heat exchange with the cooling fluid passing from said heat exchange.

10. A method of distillation which comprises vaporizing a liquid, condensing the resulting vapors, withdrawing unvaporized portion, circulating a cooling liquid to said condensation stage and passing portions of the liquid to be vaporized in heat exchange with said unvaporized portion and with said circulating medium passing from said heat exchange with the vapors.

11. A method of distillation which comprises vaporizing a liquid, condensing the resulting vapors, withdrawing unvaporized portion, circulating a cooling liquid to said condensation stage and passing portions of the liquid to be vaporized in heat exchange with said unvaporized portion and with said circulating cooling medium passing from said heat exchange with the vapors and controlling said heat exchange between said liquid to be vaporized and said unvaporized portion and between said liquid to be vaporized and said circulating cooling liquid so as to maintain the temperature of the said portions after said heat exchanges at the same temperature.

12. A process for absorbing heat from vapors of gasoline and higher boiling hydrocarbons which comprises circulating a heat absorbing fluid in indirect heat exchange relationship with said vapors out of contact therewith, maintaining the heat absorption characteristics of said heat absorbing fluid constant throughout said heat exchange by maintaining said heat absorbing fluid wholly in liquid state throughout said heat exchange.

13. A process for distilling and fractionally condensing petroleum oils which comprises heating the oil to a temperature to vaporize the fractions desired, passing the vapors to a fractional condensing device, circulating a cooling liquid through said device in a closed circuit and in indirect contact with said vapors, said liquid being non-volatile at the temperatures employed and being introduced to said device at a predetermined temperature to regulate the condensation to obtain a desired condensate, and cooling the cooling liquid received from said device.

14. A method according to claim 13 wherein the cooling liquid is cooled in said closed circuit by passing in heat exchanging relation with the stock to be distilled in such manner that the cooling liquid is cooled to a predetermined degree.

15. A process for distilling and fractionally condensing petroleum oils which comprises distilling the oil at a temperature to vaporize the fractions desired, passing the vapors to a fractional condensing device, circulating a cooling liquid through said device in a closed circuit and in indirect contact with said vapors, said liquid being non-volatile at the maximum temperatures to which it is subjected and being passed through to said device under conditions to cool the vapors to a predetermined degree and regulate the separation of vapors and condensate,

16. A method according to claim 15 wherein the cooling liquid is cooled in said closed circuit by passing in heat exchanging relation with the stock to be distilled in such manner that the cooling liquid is cooled to a predetermined degree.

17. A method for distilling and fractionally condensing petroleum oils comprising applying heat to distill off the desired fractions, said heat being applied in proportion to the quantity of desired fractions present in the stock, circulating a cooling liquid which is wholly non-volatile at the temperatures employed through a closed circuit in contact with said vapors for fractional condensation thereof, circulating said cooling liquid under control to cool the vapors to a predetermined degree, and cooling said cooling liquid after said vapors have been cooled and regulating the rate of circulation of said liquid responsive to the temperature of the uncondensed vapors to obtain a constant cooling effect.

18. A method for distilling and fractionally condensing petroleum oils comprising applying heat to distill oil the desired fractions, said heat being applied in proportion to the quantity of desired fractions present in the stock, circulating a cooling liquid through a closed circuit in contact with said vapors for fractional condensation thereof, circulating said cooling liquid under control to cool the vapors to a predetermined degree and then passing said cooling liquid in said closed circuit in heat exchange relation with the incoming stock to be distilled to yield up heat to said stock in proportion to the amount of heat absorbed during condensation of vapors.

19. A method according to claim 18 wherein the cooling liquid is wholly non-volatile at the temperatures employed.

20. A method for fractionally distilling and condensing hydrocarbon oils comprising distilling off the desired fractions by the application of heat to the oils in amount governed by the amount of fractions desired, pressing the distilled vapors successively through a plurality of fractional condensers, circulating a cooling liquid which is wholly non-volatile at the temperatures employed in a closed circuit successively through said condensers, automatically controlling the temperature of said cooling liquid in certain of said condensers by controlling the rate of circulation of cooling liquid responsive to the temperature of the cooling liquid in said condensers to reduce the temperature of the vapors in each of said condensers to a predetermined degree, and cooling said cooling liquid after passage from the hottest condenser.

21. A method for fractionally distilling and condensing hydrocarbon oils comprising distilling off the desired fractions by the application of heat to the oils in amount governed by the amount of fractions desired, passing the distilled Vapors successively through a plurality of fractional condensers, circulating a cooling liquid in a closed circuit successively through said condensers, automatically controlling the temperature of said cooling liquid in certain of said condensers by controlling the rate of circulation of cooling liquid responsive to the temperature of the cooling liquid in said condensers to reduce the temperature of the vapors in each of said condensers to a predetermined degree, and cooling said cooling liquid after passage from the hottest condenser by passing the same in heat exchanging relation with the incoming feed to be distilled to yield up to said feed an amount of heat in proportion to that absorbed in the condensers.

22. A method for fractionally distilling and condensing hydrocarbon oils comprising distillling ofi the desired fractions by the application of heat to the oils in amount governed by the amount of fractions desired, passing the distilled vapors successively through a plurality of fractional condensers, circulating a cooling liquid which is wholly non-volatile at the temperatures employed in a closed circuit successively through said condensers, automatically controlling the temperature of said cooling liquid in certain of said condensers by controlling the rate of circulation of cooling liquid responsive to the temperature of the cooling liquid in said condensers to reduce the temperature of the vapors in each of said condensers to a predetermined degree, and cooling said cooling liquid after passage from the hottest condenser by passing the same in heat exchanging relation with the incoming feed to be distilled to yield up to said feed an amount of heat in proportion to that absorbed in the condensers.

23. A process of distilling and fractionally condensing oils which comprises distilling the oils so that the vapor issuing from the still has a predetermined temperature, condensing the vapors wholly with a liquid by indirect heat exchange non-volatile at the temperatures employed, circulating said condensing liquid in a closed circuit, the temperatures of the vapors and of the condensing liquid being constant at predetermined points in the system.

24. A process of distilling and fractionally condensing oils which comprises distilling the oils so that the vapor issuing from the still has a predetermined temperature, condensing the vapors with a liquid non-volatile at the temperatures employed, circulating said condensing liquid in a closed circuit, the temperatures of the vapors and of the condensing liquid being constant at predetermined points in the system, and cooling the condensing liquid after condensation of the vapors by passing the same in heat exchanging relation with the incoming oil to be treated.

25. A process for distilling and fractionally condensing hydrocarbon oil which comprises, preheating said oil by heat exchange with a circulating oil, heating said oil to a predetermined temperature to vaporize said oil, automatically regulating the. temperature to which the oil is preheated and to which the oil is heated to control said vaporization, fractionally condensing said oil vapors by heat exchange with said circulating oil and automatically controlling the temperature of condensation to control fractional condensation, said automatic regulation of preheating and condensing being efiected by controlling the circulation of said circulating oil which is substantially non-volatile at the temperature of preheating and condensation.

26. A process for distilling and fractionally condensing hydrocarbon vapors which comprises cooling the vapors issuing from a successive number of stills in a successive number of heat exchangers connected respectively to the stills, the heat exchange medium being a liquid nonvolatile at the temperature used, such heat exchange medium travelling in a closed circuit, absorbing heat from the vapors and giving up its excess heat by heat exchange relationship with incoming stock to be distilled.

2.7. A method according to claim 26 wherein the heat exchange with the incoming stock is independent of the rate of feed of said stock.

28. An apparatus for distillation comprising a vaporizing unit, means for introducing fluid to be vaporized to said unit, a condensing unit as sociated with said vaporizing unit, means for passing cooling fluid to said condensing unit and means for passing cooling fluid from said con- 5 densing unit in heat exchange to the fluid passing to the vaporizing unit.

29. An apparatus for distillation comprising a vaporizing unit, means for introducing fluid to be vaporized to said unit, a condensing unit associ- 10 ated with said vaporizing unit, a bulk supply for cooling fluid, means for passing cooling fluid from said bulk supply to the cooling unit and means for passing cooling fluid from said condensing unit in heat exchange with the fluid to 15 be vaporized and means for returning said cooling fluid to the bulk supply.

30. An apparatus for distillation comprising a vaporizing unit, a condensing unit, connections therebetween, a vapor line from said condensing unit to a second condenser, a bulk supply for cooling fluid, means for circulating a cooling fluid from said bulk supply to said first condensing unit, means for regulating the flow of cooling fluid to said condensing unit responsive to the temperature in said conduit leading to said second condenser, means for passing said cooling fluid from said condensing unit in heat exchange with fluid passing to said vaporizing unit, means for returning the fluid from said first condensing unit to said bulk supply.

31. An apparatus for distillation which comprises a source of supply of oil to be vaporized, means for passing said oil at controllable rate through a plurality of heat exchange elements in heat exchange with unvaporized material passing from said distillation unit and in heat exchange with cooling fluid circulating in said distillation apparatus, means for introducing said feed material into a vaporizing element to separate the liquid into a vapor and unvaporized fractions, means for rectifying said vapor, means for commingling the unvaporized portion from the rectifying and from the vaporizing element, means for introducing said commingled fractions 46 into a stripping tower to pass in counter-current with vapors generated from the unvaporized fraction in said stripping tower, means for passing said vaporized fractions from said stripping tower into a vaporizing element to generate the vapors 50 to be introduced into said stripping tower, means for withdrawing the unvaporized portion from said last mentioned vaporizing element and means for passing said unvaporized portion to the first mentioned heat exchange element adapted to pass said unvaporized fraction in heat exchange with the incoming material to be distilled, means for removing the vapors from said stripping tower and rectifying same, means for returning at least a portion of the unvaporized portion from the last mentioned rectifying means into said stripping tower, means for condensing the vapors from said rectifying unit, a bulk supply for a cooling fluid, means for circulating said cooling fluid from said bulk supply into the aforementioned condensing unit and to the aforementioned heat exchange element in heat exchange with the incoming fluid to be vaporized and means for returning said cooling fluid back to said bulk supply.

ALEXANDER GRIFFITH PAGE. 

